Charging of preheated coal into the coking chambers of a coke oven battery



July 22, 1969 l.. D. SCHMIDT CHARGING OI'x PREHEATED COAL INTO THE COKING CHAMBERS OF A COKE OVEN BATTERY 3 Sheets-Sheet l Filed July 20, 1964 INVENTOR.

ATTORNEY.

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United States Patent O 3,457,141 CHARYGING OF PREHEATED COAL INTO THE COKING CHAMBERS OF A COKE OVEN BATTERY Lawrence D. Schmidt, New York, N.Y., asslgnor to Allied Chemical Corporation, New York, N.Y., a corporation of New York Filed July 20, 1964, Ser. No. 383,750 Int. Cl. Cb 47/18, 3.7/02

U.S. Cl. 201-10 Claims ABSTRACT OF THE DISCLOSURE A method of charging hotvoperating coke ovens in a battery on a cyclical basis wherein coarsely commmuted coal is conveyed via closed pipeline at stated velocity and is discharged into the oven in an atmosphere of conveying gas to form a cushion in the oven togive a umform average rate of charge to fill the oven 1n a defined time 1nterval.

consequent marked increase in the capacity of the battery for this reason and also'because the chargingof dry coal enables the charging of more coal per unit volume of the coking chamber. When coal containing moisture 1s mtroduced into the coking chambers the amount of heat required to be transferred through the walls of each chamber to and through the stationary charge to evaporate the water content of the charge is indeed large. About 40% of the total coking time is spent, in prior conventional coking practice, to effect the necessary heat input throughout the charge to evaporate and remove the water content of the charge and to raise the temperature thereof to within the range of from 250 to 700 F. In modern practice, `with large coking chambers having a capacity, say, of about 15 to 25 tons per chamber, the coking time is usually from about 15 to 30 hours depending on the type of the coke produced, namely, whether blast furnace coke or foundry coke. A saving of 40% of this time is indeed'of vast economic importance. The charging of preheated coal also improves'the quality of the coke, especially in the case of coals of higher oxygen content, such as Illinois coals. n I 1t has been'proposed to preheat the coal in a fluidized state in a fluidizing and heating chamber externally of the coking chambers of the battery to a temperature ofabout 700 F. and then convey the preheated fluidized coal particles by the uidizing gas into the coking chambers of the battery, where carbonization of the preheated coal is effected (United States Patent 2,658,862). This procedure is objectionable for a number of reasons, among which may be'mentioned that it requires the pulverization of the co'al to reduce it to a particle size (65% minus 200 mesh) such that it can be fluidized and conveyedby the uidizing gasfThe coking of such fine coal results in coke of poor quality, unsatisfactory for many metallurgical uses. Because of the low bulk density of such necoal, the charge per unit volume of coking chamber is much lower than the charge per unit volume 'of coarsely comminuted coal particles, such as are commonly used'for charging the coking chambers.

The feed of preheated coal by means of an inert gas 3,457,141 Patented July 22, 1969 such as coal gas, as disclosed in my Patent 3,047,473, leaves much to be desired from the standpoint of effecting the charging of the coking chambers reasonably smoothly and within a reasonable time, say not exceeding about 20 minutes for each coking chamber having a capacity of about 15 to 25 tons or more, without excessive carry-over of fine coal particles in the collector main of the oven battery and without excessive power requirements for the compressor or compressors required to compress thenert gas to the pressure necessary for effecting the transport of the preheated coal particles into the coking chambers.

The introduction of preheated coal employing a conventional larry as heretofore carried out involving the relatively rapid dumping of the charge into the coking chamber, usually in about one or two minutes, has the serious objection that as the mass of hot coal enters the hot coking chamber it may catch fire with consequent damage to the larry car. Such rapid charging has the disadvantage of introducing excessive quantities of suspended particles in the gas taken off from each coking chamber.

The problems involved in effecting feed of the preheated coal from the preheater into the coking chambers to supply each chamber with the desired charge of the order of 15 to 25 tons or more in the case of modern coke oven batteries, which may contain from 20 to 90 coking charnbers, are indeed manifold. Necessary precautions must be observed to prevent hot coal particles from catching fire. Obviously, air or oxygen-containing gases cannot be used as the carrier gas and hence ordinary pneumatic transport employing air as the carrier gas in out of the question. The feed of the hot coal must (a) be smooth and free of interruption into the coking chamber being charged; (b) be reasonably rapid so that the charging can lbe effected within a reasonable time period, permitting successive charging of the chambers after pushing the coke therefrom to provide the empty chamber for charging; (c) be under conditions avoiding excessive carry-over of ne particles into the collector main; (d) avoid a smoke nuisance; and (e) not interfere with the collection of coke oven gas in the collector main from other coking chambers at progressively different stages of coking.

It is a principal object of the present invention to provide a novel procedure of charging the coking chambers of coke oven batteries with coarsely comminuted, preheated coal particles so as to effect such charging smoothly and efficiently.

The use of coarsely comminuted coal, rather than lfine coal, permits the attainment of a satisfactory bulk density of the coke oven charge. l

Other objects and advantages of this invention will be apparent from the following detailed description thereof.

ln accordance with this invention, coarsely comminuted coal particles, of a particle size conventionally used'for charging the coking chambers of a battery and preheated to a temperature within the range of from 250 `to 700 F. along with a carrier gas, namely, steam or coke oven gas, preferably superheated steam, in amount to provide a relatively high weight ratio of coal to carrier gas, at least 20 to 1, are charged into an empty coking chamberjat a rate such that it takes at least about five minutes to introdu-ce the entire charge into the coking chamber,` which, as noted, can have a capacity of from about `15 to 25 tons or more.

The Icoke oven gas used as the carrier gas can be .the same type `of coke oven gas as is employed in the heating v lines of the battery. It is supplied to'the preheated coal at ambient temperature. While coke oven gas can be used, steam is preferred for a number of reasons, including (a) steam reacts endothermically with carbon, thus reducing the temperature conditions during the charging with consequent reduction in evolution of volatiles during the charging, and (b) steam condenses in the hydraulic main, thus lessening the problem of maintaining proper pressure in the hydraulic main during charging. The description which follows will, therefore, be confined chiey to the use of steam as the carrier gas with the understanding, however, that coke oven gas can be used instead of steam.

Desirably, before the charging of the coal-steam mixture is commenced, steam, preferably superheated steam, is introduced into the empty hot coking chamber to provide therein a steam atmosphere. Thereafter the preheated coarsely comminuted coal particles, along with additional steam at least during the initial stages of the charging, are charged into the steam containing coking chamber so that the weight ratio of coal to steam is at least 20 to l and can be from 20 to 500 to 1 in the case of the coal-steam mixture pipe-lined into the coking chamber. As the charging continues the amount of steam introduced with the coal particles can be reduced and during the latter stages of charging, the amount of steam Acan be the minimum amount required to obtain the transport or flow of the preheated coal. Employing mechanical transport such as a larry car, after introduction of coal to carrier gas weight ratio of at least 20 to 1, results about 10% of the charge, the amount of steam introduced with the coal can be reduced to a minimum, i.e., so much so that towards the end of the charging the How of steam into the coal charge fed to the coking chamber can be discontinued.

The mixture of preheated coal and steam is introduced into the coking chamber to form therein the desired charge at a rate such that it requires at least five minutes and not more than minutes, preferably from 5 to l2 minutes, to introduce the entire charge into the coking chamber. These values are for modern coke oven batteries having coking chambers each adapted to contain from 15 to 25 tons of coal and a volumetric capacity of from 600 to 1200 cubic feet. Thus the rate of feed of the preheated coal is such as to require at least 0.4 minute and not exceeding 3.3 minutes per 100 cubic feet of the volume of the coking chamber. Stated otherwise, the rate of feed of the preheated coal is such as to give a rise of level of coal in the coking chamber of from 0.5 to 3.5 feet a minute for modern coking chambers dimensioned approximately 40 to 45 feet long, from 12 to 18 feet high, and approximately 11/2 feet Wide.

As compared with the heretofore known and conventional practice of charging coking chambers employing a larry, the rate of feed of the coal into the coking charnber by the procedure of this invention is relatively slow.

The charging time required is at least about five times r that now employed involving the dumping of a charge from a larry through the charging holes into the coking chamber. Attempts to introduce the preheated coal relatively rapidly at rates corresponding to the rates now used for charging wet coal so that the time required for each coking chamber is of the order of one to two minutes results in a large evolution of gases from the mass of preheated coal thus fed into the hot coking chamber, which gases may catch re with objectionable smoke nuisance andl excessive carry-over of coal particles into the collector main of the battery. Operating, on the other hand, under the recited conditions of relatively slow charging rate, yet not too slow to permit charging of successive coking'chambers, in a practical time cycle and in the presence of superheated steam which, at least during the initial stages of the charging envelops the preheated coal particles introduced into the hot coking chamber, eliminates flaming of the charge and gives satisfactory charging.

It is not fully understood why observance of the conditions of this invention, involving relatively slow charging so as to require at least about ve minutes for introducing the charge into the coking chamber, and the presence of super-heated steam or coke oven gas, preferably steam, enveloping at least the preheated coal particles initially introduced into the hot coking chamber with a in satisfactory charging of the preheated coal. As the coal is initially introduced into the hot chamber, the coal tends to form an initial thin layer covering the hot walls and floor of the chamber. This black layer later becomes the outer portion of the mass of coke produced in-the coking chamber but initially serves to retard the ow of heat from the hot walls of the battery into the remainder of the charge introduced. This factor plus the relatively slow rate of preheated coal introduction reduces the rate of volatile evolution from the preheated coal sufficiently to prevent objectionable flaming and permits the collector main or mains to accommodate the volatiles evolved during the charging.

In accordance with apreferred embodiment of this invention, the preheated coal, .superheated steam mixture is fed to the coking chambers through a pipeline provided with branches with at least one branch leading into each coking chamberrThe invention, however, is not limited to this mode' of transport of the preheated coal into the coking chamber. Other modes of effecting the feed of the preheated coal into the coking chamber, such as larry feed with slow charging and the disclosed coal to carrier gas weight ratio can be used.

In the preferred embodiment, transporting from one to three tons of preheated coal per minute through apipeline of six inch diameter, the coal being unscreened and having a maximum particle size of about one inch, i.e., the coal being coarsely comminuted, the coal and superheated steam at a pressure of from 4 to 50 p.s.i.g., preferably 5 to 30 p.s.i.g., are first introduced into the upstream end of the pipeline. The pressure Within the pipeline at the upstream end is from 4 to 50 p.s.i.g. and the velocity of the steam, preheated coal mixture within the pipeline is from l0 to 200 feet per second. Steaml jets for impelling and dispersing the coal are positioned in the bottom of the pipeline to produce high velocity jets of steam at an angle of from 5 degrees to 20 degrees to the horizontal and in a direction the same as the desired direction of ilow of the preheated coal through the pipeline. Steam is supplied to these jets at pressures ranging from 2S to 600 p.s.i.g. Along the length of the pipeline, at the bottom thereof, i.e., at the outside of the pipeline on curved sections desirably having a radius of curvature of at least about six feet and at the true bottom on straight horizontal runs, the spacing of these jets is from 6 inches to 36 inches apart, preferably 12 to 18 inches apart. The jets are spaced somewhat closed in the bends, eg., every 5 degrees to 9 degrees of arc. At least 10 jets are positioned in a degree bend having a six foot radius which corresponds to one jet every l2 inches, although preferred spacing is one jet every six or seven inches. A larger radius of curvature permits larger spacing of the jets.

In each jet the steam expands to at least sonic and preferably supersonic velocity, and thusy imparts an impulse to the coal particles in the desired direction of flow through the pipeline, thus aiding the flow. In other words, the energy of the sonic or supersonic Velocity of the jets is converted into impulses aiding the transport of the solid coal particles from one jet to the next and thus through the pipeline. Under the conditions herein disclosed, relatively low pressure conditions are maintained throughout the pipeline within the range of from` 0 lto 50 p.s.i.g. and velocities which do not exceed about 200 feet per second. The introduction of superheated steam through jets `spaced as herein disclosed avoidsthe necessity of excessively high pressures at the entry to the pipeline.

I have found that lthe, rate of flowrof unscreened hammer-milled coal throughua horizontal pipeline six` inches in diameter and 13,0 feet long, equipped with triple holed jet plugs, spacedV 8 inches apart, is given by the following empirical relationship:

Wherein: R=rate of flow of coal in tons per minute P=pressure in p.s.i.g. in the measuring bin supplying the hot coal to the feed end of the pipeline (i.e., bin 35 in FIGURE 1). l

Employing a relatively long pipeline, in the case of large batteries or where one and the same pipeline supplies more than one battery, or where the coal preheater is so spaced relative to the battery that a long pipeline is necessary, excess steam is bled off from the mixture thereof with the preheated coal particles at one or more points along the length of the pipeline to maintain the steam velocity in the pipeline below 200 feet per second and yet permit the introduction of superheated steam at a plurality of closely spaced points along the length of the pipeline to aid the transport lof the coal particles through the pipeline. Preferably, the excess steam is bled oif by subjecting the mixture to centrifugal force, for example, by ow through a curved section of the pipeline or by passing a side stream of the mixture through a cyclone separator, to produce a body of steam substantially free of coal particles. Steam is vented ffrom this body thereof substantially free of coal particles. Where a side stream is removed, coal particles carried thereby can be returned to the pipeline.

The venting or bleeding off of the steam from the pipeline as herein disclosed permits replacement thereof along the length of the pipeline by the steam introduced at sonic or supersonic velocities in the form of jets to aid the propulsion of the coal particles through the pipeline, and this without excessive build-up of velocity of mixture of coal and superheated steam in the pipeline. The number of such venting units employed in any pipeline will depend on the particle size of the coal particles transported, the length of the line, the quantity of steam jetted thereinto, and the pressure in the feed tank at the head of the pipeline. For any given pipeline, it is a comparatively simple matter to determine the number of such venting units which should be used for optimum ow of the preheated coal particles. In general, two units should be used per 100 feet of pipeline length when conveying preheated hammer-milled coal in a pipeline having an inside diameter of six inches employing steam as the carrier gas supplied to the jets under a pressure of from 150 to 600 p.s.ig., the steam jets being spaced apart approximately inches between adjacent jets. The steam upon entering the pipeline through the jets expands to at least sonic velocity when the absolute pressure of the steam supply is at least twice that of the absolute pressure in the pipeline.

At least one steam venting unit should be positioned at a point where the pipeline communicates with the branch leading into the coking chamber. Each branch leading into a coking chamber can itself be shaped to produce a curved bend subjecting the mixture flowing therethrough to centrifugal force to produce in thebend a body of steam substantially free of coal particles, which body is vented either to the atmosphere or to an adjacent coking chamber or to a condenser. Thus the mixture which is charged into the coking chambers has a high ratio of preheated coal particles to steam. This facilitates disentrainment of the coal particles from the steam within the coking chamber and hence minimizes carry-over of coal into the gas off-take.

Good transport through the pipeline is obtained when the ratio of preheated coal particles to steam on a weight basis at the inlet end of the pipeline, is to k350, pref-v erably about 80; in the pipeline, up to the discharge point into the coking chamber, is 20 to 150, preferably about 60, and upon discharge into the coking chamber is 20 to 500, preferably about 80.

steam at the charging inlet end of the coking chamber (the end `of the chamber where the preheated coal enters) is limited to the range of -1/2 to 2 p.s.i.g. The opposite end of the coking chamber can be vented to the collector main or to an adjacent coking chamber during the charging to insure that the pressure at that end is less than that on the charging end of the chamber. In the case of new batteries built to practice this invention, which can be built without charging holes in the lroof and which have only one collector main at the opposite side of the battery from that containing the coal inlets, such differential pressure can be created by not venting the charging end of each coking chamber during the charging and letting the pressure build up to the desired extent which the opposite end of the chamber is in communication with the collector main. Existing batteries require the sealing of the charging holes at the charging end of the coking chambers to prevent leakage of gas through these charging holes which would prevent pressure build-up to within the range of from y1/2 to 2 p.s.i.g. This differential pressure within the coking chamber during charging tends to eifect the distribution of the charge through-out the length of the charnber and gives a charge which does not require leveling. In other words, the pressure differential facilitates the charging of the far end of the oven chamber with disposition of the charge into the coking chamber throughout its length to a reasonably uni-form height so that leveling of the charge with a leveling bar is not necessary. b

In the accompanying drawings forming a part of this specification and showing for purposes of exemplifcation a preferred embodiment of this invention without limiting the claimed invention to such illustrative instance:

FIGURE 1 is a flow sheet, diagrammatic in character, showing a preferred layout of equipment for supplying preheated coal to the coking chambers of a battery;y

FIGURE 2 is a fragmentary perspective of a coke oven battery showing the preferred technique for transporting the preheated coal to the coking chambers of the battery;

FIGURE 3 is a fragmentary vertical section through a coking chamber of an existing battery modied for charging by the present invention;

FIGURE 4 is a fragmentary vertical section through a coking chamber showing a charging larry in position to charge the coking chamber, which larry is designed to effect the charging in accordance with the present lnventlon;

FIGURE 5 is a fragmentary sectional view, on an enlarged scale as compared with the scale of the other figures, through a portion of the pipeline showing one of the jet nozzles; and

l FIGURE 6 is a fragmentary sectional view through the pipeline, at right angles to the section of FIGURE 5 and showing a plan view of a jet nozzle in the pipeline.

Referring to FIGURE 1, wet coal containing` from 3% to 12% by weight of moisture, usually` from 7% to 8% moisture, is supplied by a conveyor 10 to the coal bin 11. This wet coal is the usual vhammer-milled coal employed in charging the coking chambers of the coke oven battery, i.e., coarsely comminuted, the particles of which are less than one inch in size in their greatest dimension and usually of a particle size such that from 3% to 20%' of the particles are larger than about 1A inch; from 8% to 40% of the particles are larger than 1A; inch; and over, of the particles are larger than 0.04 inch.. In the trade this size of coal is referred to as .to `90% through a Ms inch screen. It is the particle size commonly used for charging the coking chambers of a battery. to produce metallurgical coke. Coals of such particle size are referred to herein as coarsely comminuted coal.

In the embodiment of the invention shown in FIGURE 1, a preheating installation is shown involving two preheaters, each with associated dust collectors. The number of preheaters used will, of course, depend on the capacity of the preheater as well as that of the coking r '7 chambers. For smaller installationsfwhere one preheater will produce preheated coal at a temperature within the range of fromA 250 to 700 F. in suticient quantity to supply the coking chambers of the battery, then the installation need have only one such preheater or, if desired, a second as a standby unit. Larger installations will, of course, have more than one coal preheating unit.

Since both preheating units 12 of FIGURE 1 are the same, only one will be described in detail. Each unit comprises a heater 13, desirably in the form of the well known Herreschoff fumace,` comprising a series of superimposed hearths 14 over which rabble arms 15 rotate to effect the discharge of the coal from an upper hearth to a lower hearth. Hot combustion gases produced in the combustion chamber 16 supplied with fuel through line 17 and air through line 18 to support combustion enter the base of-the heater 14 and ilow upwardly countercurrent to the descending coal. The heaters 13 can be of any known type in which effective preheating of the coal is effected to a temperature within the range of from 250 to 700 F.; the Herreschoi type represents one such heater.

The preheated coal at a temperature within the range of from 250 to 700 F. is Withdrawn from the base of the heater through line 21 which enters the topi of receiving bin 22. Hot combustion gases leaving the heater exit through line 23 into a cyclone separator 24, desirably a dual unit of known type. Coal entrained in the hot gases settle out in this cyclone separator 24 and is discharged through valve controlled line 25 into the hot coal line 21.

Exhaust gas from the cyclone separator 24 is pumped through line 26 into a dust collector 27 which can be of the cyclone separator type. In dust collector 27 solid particles are separated and are discharged through valve controlled line 29 into the coal feed line 21. The substantially dust-free gas can be discharged into the atmosphere through line 31.

C1 is a control of known type which controls the amount of fuel supplied through line 17 responsive to the temperature of the preheated coal to maintain the temperature of the latter substantially constant. C2 is a control of known type which controls the volume of exhaust gas recycled through line 26' to the combustion chamber 16 where this-exhaust gas mixes with the combustion products and thus tempers the temperature of the combustion gases supplied to the heater 13 and maintains the temperature of the combustion gases at the desired value. Each heater is equipped with an oxygen analyzer unit of knowntype to insure that the combustion gases entering the heater are free of oxygen. The preheaters can be supplied with additional conventional temperature and pressure controllers and electrical interlocks to insure proper sequence of operation under selected conditions of temperature and pressure for optimum performance of the preheating equipment.

Receiving bin 22 discharges the preheated coal to an elevating conveyor 32 which delivers the preheated coal into a measuring bin 35. Measuring bin 35 is of suicient capacity to maintain therein preheated coal in amount to supply the desired complete charge for charging an empty coking chamber. Measuring bin 35 is periodically filled from the receiving bin 22 which has an appreciably larger capacity than the measuring bin 35. In storage or receiving bin 22 is stored enough of the preheated coal to insure smooth operation, i.e., to supply the measuring bin 35 at intervals depending upon the charging cycle withthe correct amount of preheated coal to supply the desired charge to the coking chamber being charged. When this-amount of coal is introduced into the measuring bin 35, thevalve 34 is closed to seal the measuring bin.l ,Steam'is thenl introduced into the measuring bin through `line S (FIGURE 2), having a valve S1 therein, to produce .a mixture ofsteam and coal particles which will owreadilyfeg., a mixture under a pressure of fronr4 to 50 p.s.i.g.

Measuring bin 3S has at its discharge end a crusher 36 which can beof any desired type, such, for example, as the crusher disclosed in my co-pending application Ser. No. 282,351, filed May 22, 1963, and now abandoned. The crusher when used, has the function of crushing any oversized particles or agglomerates, thus insuring the delivery to the accelerator chamber 37 of coal well dispersed'in the carrier gas having a maximum particle size conducive to trouble-free transport through the pipeline into the coking chambers. In the embodiment shown in FIGURE 2, the crusher comprises one set of crushing arms 41 eachl mounted for rotation on shaft 42 and cooperating with a second set of crusher arms 43 mounted for rotation on shaft 44. The arms 41 and 43 are arranged to rotate in inter-engagement relation as indicated diagrammatically in FIGURE 2 so as to agitate the hot coal and crush oversize lumps. A valve 45 is mounted just above the crusher 36 and controls the ow of hot coal and steam from measuring bin 35 into the crusher 36.

As shown in FIGURE 2, the accelerator chamber 37 is of truncated conical shape and has a steam jet 52 near the lower end thereof. The base of this chamber where it joins the inlet end of the pipeline 38 is of the same diameter as this inlet end. The joint between the two is such that streamline flow takes place from the exit of the accelerator chamber 37 into the pipeline 38. This joint is free of any obstructions to ow therethrough. The length of the portion of the accelerator chamber 37 from the exit of the crusher to the discharge end of this chamber is at least sufficient to permit accelerative fall of the mixture of coal particles and steam from the crusher 36 into the inlet end of the pipeline without any tendency for accumulation or packing of the coal particles to take place in the accelerator chamber. This is important because by having this distance so dimensioned, accumulation of coal particles in the lower end of the accelerator chamber, which if permitted to develop would tend to obstruct or clog the flow into the pipeline, is prevented. Acceleration of the coal in a gravity type accelerator has been shown in the drawing and described above. However, other types of accelerators can be used, such, for example, as the known mechanical slingers.

The dimensions of the accelerator chamber as well as of the pipeline, the drier and associated equipment will of course, vary for each installation and in general depend on the capacity of the coking chambers, the charging cycle used and the size of the coal particles charged.

In the embodiment of the invention shown in FIG- URES 2 and 3, pipeline 38 has an inside diameter of from 4 to 8 inches, preferably about 6 inches, and leads from the exit end of the accelerator chamber 37 to a manifold 47 which extends along the length of the battery. Manifold 47 has a discharge conduit or branch 48 individual to each cokingA chamber leading into one end of that coking chamber, preferably at an angle of less than about 23 degrees to the horizontal so that the coal-steam mixture is discharged into one end of the coking chamber and ilows therefrom towards the opposite end of the coking chamber, disentrainment of the coal from the steam taking place as the coal is fed into the coking chamber.

As customary, the coking chambers, a section through one'of which is shown in FIGURE 3, are each provided with doors 49 at the opposite ends. The usual gas ofttake 50 leadsirito a collector main -M (FIGURE 4) from the opposite end of the coking chamber from that into which the coal-superheated steam mixture is introduced. Existing batteries to which this invention may be applied customarily have charging holes H in theV roof thereof which areequipped with thefusual charging hole covers H(FIGURE 3). v

r Pipeline 38, manifold 47 and each branch 48 are each provided, at a plurality of closely spaced points along their lengths, with jet plugs 52 for introducing superheated steam. These jet plugs 52 are communicably connected with a steam line 53 through branches 54 each equipped with a valve 55. Steam line 53 is positioned adjacent pipeline 38, manifold 47 and each branch 48 to supply them with steam under a pressure of from 25 to 600 p.s.i.g. through the jet plugs 52 spaced as hereinabove disclosed. The steam is jetted into the line in the direction of ow therethrough. For example, in the case of the pipeline 38, as shown in FIGURE 5, in which the arrow 56 indicates the direction of flow through the pipeline, and arrow 57 the direction of steam jet ow into the pipeline, the steam enters at sonic or supersonic velocities and imparts impulses to the owing mixture, aiding the ow through the pipeline; thus the sonic or supersonic velocity of the steam at the point of entry is immediately transformed into the energy imparted to the hot coal-superheated steam mixture to aid ow from one jet to the next. The pressure within the pipeline 38 and manifold 47 remains Within the range of from 0 to 50 p.s.i.g. and the velocity of the coal-steam mixture below 200 feet per second.

The valves 55 in branches 54 can be adjusted to give the desired sonic or supersonic velocity of flow into the pipeline or can be closed when it is desired to reduce the number of branches supplying fresh steam to the pipelines.

A preferred form of jet plug 52 is shown in FIGURES and 6 and comprises a hexagonal plug 61 having a threaded end 62 in threaded engagement within a bore 63 in the wall of the pipeline 38 or manifold 47. The top of threaded end 62 lies flush with the inner wall of the pipeline to provide a smooth interior where the jets enter the pipeline or manifold free of obstruction to the flow of the steam-coal mixture and also free of pockets or dead spaces. Plug 61 has a nozzle 64 or a group of such nozzles 64, each of venturi shape having a divergent or exit portion 65, the included angle formed by the walls of which is between 5 and 7 degrees and having an entrance portion that is effectively convergent. In the embodiment shown in FIGURES 5 and 6, each plug 52 has three such nozzles communicating with a passage 67 leading into a central bore 68 in plug `61. Preferably each nozzle delivers a jet of superheated steam at an angle of about 5 to 20 degrees with respect to the axis of the pipeline at the point Where the jet nozzle is positioned, e.g., in the case of a straightaway or horizontal pipeline, at an angle of about 5 to 20 degrees with respect to the horizontal. The end 69 of each plug 52 is threaded at 71 to receive the threaded end 72 of a branch 54 leading from the steam line. This arrangement provides fan-like jets of steam imparting velocity or impulses to the owing mixture of preheated coal and superheated steam in the direction of ow indicated by the arrow 56 (FIGURE 5).

The manifold 47 extends the full length of the battery, along one side thereof, desirably the side opposite to that on which the collector main is positioned. Each branch 48 leading from the manifold 47 is individual to a coking chamber 75 of the battery. Each branch 48 is of arced or curved shape; the radius of curvature is preferably about six feet. The exit end 76 of the branch extends into the refractory roof of the battery and leads into a down- Wardly inclined passageway 77 (FIGURE 3) in open communication with a coking chamber 75. The angle of inclination to the horizontal of the exit end 76 and the passageway 77 is such as to direct a flowing stream of superheated steam and preheated coarsely comminuted coal particles in a downwardly inclined direction toward the opposite end of the coking chamber. An angle less than about 23 degrees to the horizontal (i.e., the angle formed between the axis of the passageway 77 and the horizontal) gives satisfactory charging. While in FIG- URE 3 the passageway 77 is shown leading into the lower end 78 of a charging hole H, the passageway 77 need not communicate with a charging hole. FIGURE 3 shows a construction applied to an existing oven battey having charging holes H, three in number, spaced across the top of each coking chamber. In the case of new batteries, to which this invention is applied, the roofs of the coking chambers need not have any charging holes therein.

As noted, each branch 48 has a plurality of closely spaced steam jet plugs 51 therein. The spacing of the jets is the same as in a curved section of the pipeline. For the Sake of carity of illustration, all of the jets in the pipeline 38, manifold 47, and each branch 48, have not been shown on the drawing.

Flow through each branch 48 from the manifold 47 is controlled by a pair of valves 81 and 81. Valves 81 are positioned in the manifold 47 and control ow through this manifold to the branch 48 leading into the coking chamber to be charged. Thus all valves 81 in the portion of manifold 47 leading up to the branch 48 communicating with the coking chamber to be charged are open and at least the valve 81 in the manifold 47 immediately following the branch leading into the coking chamber to be charged is closed. Thus the coal-superheated steam mixture must ow into the branch communicating with the coking chamber to be charged. Each branch 48 has a valve 81 at the inlet end thereof which controls the flow from manifold 47 thereinto. Each valve 81 and 81' is equipped with a pressure fluid cylinder 82 or effecting actuation thereof. Valves 81 and 81 controlling ow into a coking chamber to be charged are opened when that coking chamber is empty and in condition for charging; these valves are closed when the charge has been introduced into that chamber. Valves 81 and 81 of the respective branches 48 and the rest of the equipment can be operated through suitable timing mechanism so that automatic introduction takes place of superheated steam into the successive empty hot chambers, followed by the feed thereinto of preheated coal-steam mixture, as well as the feed of the preheated coal into the measuring bin 35 from the receiving bin 22 and into the latter from the preheater 12.

`Preferably, but not necessarily, each branch 48 is equipped with a bleed-olf 83 leading from the inner curved portion 84 of the branch into an adjoining coking chamber 75, i.e., the bleed-off leads into a coking chamber adjoining the chamber receiving the charge. As the mixture of superheated steam and preheated coal flows through the curved portion 84, it is subjected to centrifugal force so that substantially all of the coal particles tend to concentrate in the locality of the outer wall of the curved portion 84, i.e., the wall remote from the port or opening leading into the bleed-off 83. Hence in the vicinity of the inlet to the bleed-off 83, the superheated steam is substantially free of coal particles. This superheated steam flows through the bleed-olf 83 into the adjoining chamber which is in an advanced stage of the coking and hence can readily accommodate the carrier gas which ows from that coking chamber into the collector main.

The bleed-olf of superheated steam from the coalsteam mixture flowing into the coking chamber being charged increases the coal to steam weight ratio of the mixture charged into the steam-containing coking chamber. This facilitates disentrainment of the coal from the steam. The steam entering the chamber being charged upon disentrainment from the coal particles exits through the uptake leading into the collector main. The steam entering the adjacent chamber or a pair of chambers on the opposite sides of the coking chamber being charged, if desired, flows across the open space above the coke in these chambers and exits from these chambers through the gas olf-takes into the collector main. Any solid coal particles therein, for the most part, settle out and become part of the coke charge in the adjacent chambers.

In operation, after the preheated coal is introduced into the measuring bin 35 in amount to supply a charge for a coking chamber, valve 34 is closed. Valve 45 had been closed previousy. The valves 81 and 81 controlling flow to the branch leading to the coking chamber to be charged are opened while closing the valves 81 in the coal manifold downstream of the coking chamber being charged. Steam is turned on to the jets upstream of this coking chamber. The Crusher is actuated; valve 45 is opened and steam is supplied, preferably, to the lower part of bin 35 to raise it to desired pressure, e.g., 4 to 5() p.s.i.g. The steam jets upstream of the coking chamber being charged serve to produce a steam atmosphere in the coking chamber to be charged. The formation of such steam atmosphere in each coking chamber before introduction of the hot coal charge thereinto represents preferred operation, although satisfactory charging can be eected by not lling the cokingchamber to be charged with steam prior to the commencement of the feed of the coal-steam mixture into that coking chamber. Thereafter coal ow to the oven begins and continues at a rate to introduce the charge in from about to 12 minutes.

In the case of a long pipeline, say exceeding 100 feet in length, the line is provided with a curved portion 91 which can be in the form of a horizontal curve, i.e., lie in a horizontal plane as shown in FIGURE 2, or a vertical curve. This curved portion 91 desirably is made up of successi-ve curved sections A, B and C designed for streamline flow therethrough. The radii of curvature of adjacent portions A and B, and B and C are diametrically opposite each other. For a six inch pipeline the radius of curvature is preferably about six feet. As the mixture of preheated coal and superheated steam flows through the curved portion 91, it is subjected to centrifugal force causing the coal particles to concentrate in the locality of portion 92 and forming opposite this locality at 93 a body of steam substantially free of coal particles. A bleed-olf or vent 94 is provided for bleeding off steam from this body, thus removing enough of the superheated steam to avoid excessive velocities in the pipeline and to enable the introduction of superheated steam through the subsequent jets in the direction of ow of the superheated steampreheated coal mixture without creating excessive velocities within the pipeline, the manifold 47 and the branch 48 leading from the manifold into the coking chamber to be charged.

Aften initiation of the introduction of the mixture of preheated coal and superheated steam into the coking chamber, the pressure of the steam released from the mixture can be permitted to build up in -the end of the coking chamber where the mixture is introduced. That is to say this end of the coking chamber is not vented. -In the case of an existing battery having charging holes, modified to practice this invention, percautions are taken to insure that the charging hole covers at the end of the coking chamber which receives the charge are tightly sealed to enable the pressure in that end of the chamber to build up to within the range of from 1/2 to 2 p.s.i.g. The opposite end of the coking chamber communicating with the usual gas olf-take at the opposite end of the coking chamber is thus at a lower pressure. This opposite end of the coking chamber is usually vented through the olftake to the collector main during the charging. The differential pressure thus created between the respective ends of each chamber during the charging thereof facilitaties the ow of the coal-steam mixture from the end of the chamber Where it is introduced to the opposite end and gives a distribution of the coal within the coking chamber so as to produce a reasonably uniform level of coal throughout the length of the coking chamber, i.e., a disposition of the charge requiring no leveling. Hence while the present invention is not coniined to charging without leveling, it enables such charging to be eiected.

When the measured charge has been delivered from the measuring bin 35, valve 45 is closed. When this charge has been introduced into the chamber being charged, the steam jets 52 are turned off and the operation of the Crusher 36 interrupted. Valve 34 is then opened and a fresh charge of preheated coal introduced from the reciving bin 22 into the measuring bin 35S. Once this charge has been introduced into measuring bin 35, the operation hereinabove described is repeated for the next coking chamber Ito be charged.

During the charging of each chamber, in the embodiment shown in FIGURE 2, branch 48 is vented into an adjacent coking chamber through bleed-off S3, thus reducing the steam input into the chamber being charged, i.e., increasing the weight ratio of coal to steam introduced into the coking chamber being charged. Higher coal to steam ratios facilitate disentrainment of the coal from the steam and tends to reduce the charging time. It also tends to prevent carry-over of -ine coal particles by the steam introduced into the chamber being charged from that chamber into the collector main. Bleed-olf 83 can be provided with a valve to control iiow therethrough or to permit optional use of this bleed-olf.

Bleed-olf 83 can be designed to connect with two adjoining coking chambers to vent steam into these two chambers. Operating in this manner facilitates recovery of coal particles carried by the steam thus vented into the adjacent chambers, which coal particles form part of the coal charge in these adjacent chambers and are eventually converted to coke.

With relatively high coal to steam ratios, the venting of the steam-coal mixture introduced through branch 48 into the chamber being charged can be eliminated entirely. As a general rule, venting into one adjacent coking chamber is useful in minimizing carry-over of coal particles by the steam from the chamber being charged into the collector main and also in facilitating disentrainment of the coal from the steam in the chamber being charged in that it reduces the amount of steam introduced into the chamber being charged.

The following example of charging a coke oven battery, the coking chambers of which are approximately 12 feet high, 40 feet long and 18 inches wide, is given for illustrative purposes. The equipment used in substantially that shown in FIGURE 2. The measuring bin 35 after introduction of the charge of preheated coal (l5 tons) at a temperature of about 650 F. was pressurized with superheated steam to a pressure of 9.8 p.s.i.g. The crusher 36 was driven at approximately 93 r.p.m. Steam was introduced into the coking chamber to form therein a steam atmosphere. Steam was then introuced through the jets spaced along the length of the pipeline 8 inches apart in the horizontal stretch and somewhat closer in the bends of the pipeline. The total conveying steam used was 506 pounds equivalent to 79 pounds per minute. The steam pressure was 287 p.s.i.g. on the average 65.6 pounds per minute of steam was supplied to the jets in the pipeline.

The charging of the chamber required 6.4 minutes. At the end of this time the coal was disposed in the charnber in a mound with the level of the coal at the ends of the chamber about a foot below fthe level in the middle of the chamber. Upon leveling the coal was disposed at a substantially uniform height throughout the length of the chamber. The chamber which as noted was l2 feet high was lled to a height of 11.2 feet.

Such charging is repeated for each chamber of the battery by manipulation of the valves.

In the battery of FIGURE 4, a charging larry 100, having three charging hoppers i101, one for each charging hole travels on rails 102 on the roof of the battery. Each of the hoppers has a covered top which prevents access of air to the hot coal in the hopper. The cover, of course, can be removed to perimt filling the hopper with hot coal. This larry can be of a known type involving a rotary discharge plate 103 at the base of each charginghopper 101. Each plate 103 is rotated by a motor drive (not shown) as conventional, the speed of which is adjustable to give discharge of coal at the desired rate. Each discharge plate delivers the coal to a discharge chute which, as conventional, communicates with a drop sleeve 104. These sleeves in their lowered position bridge the spaces between the discharge ends of the discharge chutes and the inlet ends of the charging holes communicating therewith. Larry 100 travels along the top of the battery, receives a charge of preheated coarsely comminuted coal, preheated to a temeparture within the range of from 250 to 700 F. at the loading station for the larry and then is moved into charging position over the empty chamber to be charged.

Positioned at one side of the battery running the length thereof is a steam line 105. This line has branches 106, one individual to each coking chamber provided with a valve 107 to control flow therethrough and equipped with a conventional quick attachable and detachable coupling 108 for connection to flexible steam conduit 109 carried by the larry. Conduit 109 communi- Cates with a steam line 110 having three branches 111, one for each charging hopper :101. Each branch 111 has a flexible lower end 12 which leads into a drop sleeves 104 as shown in FIGURE 4. Conduit 109 has a ow control valve 115 therein.

When the larry is spotted over the empty chamber to be charged, conduit 109 is coupled to steam line 105. Valves 107 and 115 individual to the chamber being charged are turned on to lill the chamber with superheated steam. The steam flow is continued during the charging which is carried out at a rate such that from to 12 minutes are required to introduce the charge into the coking chamber; such charging is effected by rotating the discharge plates 103 at a rate to give the necessary slower feed of the hot coal through the drop sleeves into the coking chamber. The flow of steam into the coal passing through the drop sleeve prevents aspiration of air into the falling coal stream and thus avoids res and explosion hazards which would be involved in charging hot coal from a larry into a hot coking chamber by dumping same from the larry into the coking chamber at the relatively rapid rates normally used. The steam, with the slow charging as hereinabove described, thus serves a dual purpose. Its presence in the coking chamber when hot coal irst enters protects the dry hot coal from excessively fast carbonization which, were it to occur, would result in excessive evolution of volatiles which carry ne coal particles up through the gas off-take; also, the steam blankets the falling coal from the air thus avoiding fires and explosions.

The amount of steam introduced should be as hereinabove described to provide a relatively high coal to steam weight ratio, so that rapid disentrainment of the coal from the steam takes place in the coking chamber. The coal to steam weight ratio can be from 20 or more to 1. Coke oven gas can be used instead of steam, supplied to the larry from a coke oven gas main at ambient temperature, in amount such as to provide about the same weight ratio as in the case of steam.

While preferred embodiments have been disclosed herein and illustrated in the drawings, it will be understood this invention is not limited to this disclosure including the showing of the drawings because many variations and other modifications will occur to those skilled in the art.

What is claimed is:

1. A method of charging the coking chambers of a coke oven battery with hot, coarsely comminuted coal particles, which method comprises, preheating the coal particles in coarsely comminuted condition to a temperature within the range of from 250 to 700 F., feeding the preheated coal into a measuring bin to produce therein an amount of preheated coal equal to a desired charge for a coking chamber, introducing steam into this charge of preheated coal in the measuring bin to produce a tlowable mixture of steam and preheated coal, introducing steam into the coking chamber to be charged, thereafter feeding the owable mixture from the measuring bin into an accelerator chamber communicating with a pipeline, which pipeline in turn communicates with the coking chambers, and introducing jets of steam at closely spaced points along the length of the pipeline to effect feed of the coal-steam mixture therethrough into the coking chamber to be charged, the volume of steam thus introduced into said pipeline being such as to provide a weight ratio of coal to steam within the range of from 20 to 150.

2. The method of charging the coking chambers of a coke oven battery as defined in claim 1, in which the jets of steam are introduced into the pipeline at supersonic velocities.

3. A method of charging the coking chambers of a coke oven battery with hot, coarsely comminuted coal particles, which method comprises, preheating the coal particles in coarsely comminuted condition to a temperature Within the range of from 250 to 700 F., feeding the preheated coal into a measuring bin to produce therein an 'amount of preheated coal equal to a desired charge for a coking chamber, introducing steam into this charge of preheated coal in the measuring bin to produce a owable mixture of steam and preheated coal, introducing steam into the coking chamber to be charged, thereafter feeding the owable mixture from the measuring bin into an accelerator chamber communicating with a pipeline, which pipeline in turn communicates with the coking chambers, and introducing jets of steam at supersonic velocities at closely spaced points along the length of the pipeline to effect feed of the coal-steam mixture therethrough, venting a portion of the steam of the coalsteam mixture into an adjacent coking chamber, which portion of the steam is substantially free of coal particles while feeding the remainder of the steam admixtured with the coal into the coking chamber to be charged to effect the charging thereof, the weight ratio of coal to steam in the mixture introduced into the coking chamber being from 20 to 500 to 1.

References Cited UNITED STATES PATENTS 1,855,191 4/1932 King 201--40 1,872,883 8/1932 Byrne 201-40 2,006,115 6/ 1935 Schaefer 201-38 2,658,862 11/1953 Horner 201--31 2,794,686 6/ 1957 Anselman et al. 302--24 3,047,473 7/1962 Schmidt 201--31 NORMAN YUDKOFF, Primary Examiner D. EDWARDS, Assistant Examiner U.S. Cl. X.R. 

